JPH02241505A - Decompressed distillation method - Google Patents
Decompressed distillation methodInfo
- Publication number
- JPH02241505A JPH02241505A JP2029354A JP2935490A JPH02241505A JP H02241505 A JPH02241505 A JP H02241505A JP 2029354 A JP2029354 A JP 2029354A JP 2935490 A JP2935490 A JP 2935490A JP H02241505 A JPH02241505 A JP H02241505A
- Authority
- JP
- Japan
- Prior art keywords
- condensing section
- liquid
- taken out
- vapor
- cooling liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000004821 distillation Methods 0.000 title claims description 12
- 238000000034 method Methods 0.000 title claims description 10
- 239000007788 liquid Substances 0.000 claims abstract description 37
- 239000000110 cooling liquid Substances 0.000 claims abstract description 22
- 238000005292 vacuum distillation Methods 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims 1
- 229930195733 hydrocarbon Natural products 0.000 abstract description 8
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 8
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 7
- 230000005494 condensation Effects 0.000 abstract 8
- 238000009833 condensation Methods 0.000 abstract 8
- 238000000605 extraction Methods 0.000 description 5
- 239000000284 extract Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S203/00—Distillation: processes, separatory
- Y10S203/09—Plural feed
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S203/00—Distillation: processes, separatory
- Y10S203/20—Power plant
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
【発明の詳細な説明】
Ｌｔ−よ立五皿±１
炭化水素を含有する供給原料を蒸望する減圧蒸留方法に
圓し、供給原料は６５０から５２００Ｐａの範囲の減圧
下、３２０から４２５℃の範囲の温度を有する。供給原
料は時には古い残渣油と呼ばれるものである。DETAILED DESCRIPTION OF THE INVENTION The feedstock is distilled at a temperature of 320 to 425° C. under a reduced pressure in the range of 650 to 5200 Pa. have a range of temperatures. The feedstock is sometimes referred to as old residual oil.
（３Ｊと１菫
このような減圧蒸留法は、大気圧以下で操作する蒸留塔
の入口部に液体および蒸気を含有する供給原料を導入し
、蒸留塔の塔底部から液体を取り出し、蒸気を蒸留塔の
入口部と塔頂部の間に互いに上下に配置の少なくとも２
、つの凝縮部を通過せしめ、塔頂部から蒸気を取り出し
、各凝縮部に冷却液体を噴射し、且つ各凝縮部から液体
を取り出すことからなる。ここで各凝縮部内に噴射する
冷却液体はその凝縮部から取り出した液体からなるもの
である。(3J and 1) Such a vacuum distillation process involves introducing a feedstock containing liquid and vapor into the inlet of a distillation column operating below atmospheric pressure, removing the liquid from the bottom of the column, and distilling the vapor. At least two parts arranged one above the other between the inlet and the top of the tower.
, through two condensing sections, removing vapor from the top of the column, injecting cooling liquid into each condensing section, and removing liquid from each condensing section. Here, the cooling liquid injected into each condensing section consists of the liquid taken out from that condensing section.
各凝縮部内に噴射する冷却液体は、凝縮部を通過する蒸
気内に噴射される。その結果、蒸気の１部は凝縮し、こ
の部分は凝縮部から取り出される液体と共に蒸留塔から
取り出される。Cooling liquid injected into each condenser is injected into the vapor passing through the condenser. As a result, a portion of the vapor condenses and this portion is removed from the distillation column along with the liquid removed from the condensing section.
残りの蒸気は、真空ポンプ、例えばスチームエジェクタ
により塔頂部から取り出される。この蒸気はまだ有用な
炭化水素成分のかなりの聞を含有することが見出された
。有用な炭化水素成分のｍは、適用される供給原料の入
口温度が高いと増加する。１９８９年２月１０日出願の
英国特許出願第８９０３００７、６号に記載の減圧蒸留
装置を適用することによりこのような供給原料の高い入
口温度が可能となる。The remaining vapor is removed from the top of the column by a vacuum pump, eg a steam ejector. This vapor was found to still contain significant amounts of useful hydrocarbon components. The m of useful hydrocarbon components increases as the inlet temperature of the applied feedstock increases. Such high feedstock inlet temperatures are possible by applying a vacuum distillation apparatus as described in British Patent Application No. 8903007, 6, filed February 10, 1989.
１匪立旦］
本発明の目的は、塔頂部から取り出される蒸気の含有す
る有用な炭化水素成分が僅か少テである減圧蒸留方法を
提供することである。An object of the present invention is to provide a vacuum distillation method in which the steam extracted from the top of the column contains only a small amount of useful hydrocarbon components.
１艶匹ｌＩ
この目的のために、本発明の減圧蒸留方法は、大気圧以
下で操作する蒸留塔の入口部に液体および蒸気を含有す
る供給原料を導入し、蒸留塔の塔底部から液体を取り出
し、蒸気を蒸留塔の入口部と塔頂部との間に互いに上下
に配置の少なくとも２つの凝縮部を通過せしめ、塔頂部
から蒸気を取り出し、各凝縮部に冷却液体を噴射し、且
つ各凝縮部から液体を取り出すことからなり、ここで各
凝縮部内に噴射する冷却液体はその凝縮部から取り出し
た液体からなり、さらに最上凝縮部内に噴射する冷却液
体は最上凝縮部よりも下に配置の凝縮部から取り出した
液体からなることを特徴とするものである。To this end, the vacuum distillation method of the invention introduces a feedstock containing liquid and vapor at the inlet of a distillation column operating below atmospheric pressure, and extracts the liquid from the bottom of the column. extracting the vapor and passing the vapor through at least two condensing sections disposed one above the other between the inlet and the top of the distillation column; extracting the vapor from the top of the column; injecting a cooling liquid into each condensing section; The cooling liquid injected into each condensing section consists of the liquid taken out from that condensing section, and the cooling liquid injected into the top condensing section consists of the liquid extracted from the condensing section below the top condensing section. It is characterized by being made of liquid extracted from the plant.
添付図面を参照して実施例でさらに詳しく本発明を説明
するが、図面は減圧蒸留塔１の縦断面概略図を示す。The present invention will be explained in more detail by way of examples with reference to the accompanying drawings, which show a schematic longitudinal section of a vacuum distillation column 1.
減圧蒸留塔は、供給原料の供給導管４が入る入口部３、
出口導管７を備えている塔底部６および塔頂出口導管９
を備えている塔頂部８を含む。The vacuum distillation column includes an inlet portion 3 into which a feed conduit 4 for feedstock enters;
Bottom 6 with outlet conduit 7 and top outlet conduit 9
The column top 8 is equipped with:
減圧蒸留塔１には入口部３と塔頂部８との間に３つの凝
縮部が互いに上下に配列している。最上凝縮部は参照番
号１３、最上凝縮Ｆ１１１３から下に配置の第１の凝縮
部は参照番号１３ａおよび最上凝縮部１３から下に配置
の第２の凝縮部は参照番号１３ｂで示される。The vacuum distillation column 1 has three condensing sections arranged one above the other between an inlet section 3 and a column top section 8. The uppermost condensing section is designated with the reference number 13, the first condensing section located below the uppermost condensing section F1113 is designated with the reference number 13a, and the second condensing section located below the uppermost condensing section 13 is designated with the reference number 13b.
各凝縮部１３．１３ａおよび１３ｂには参照番号１５゜
１５ａおよび１５ｂの抽出トレイ、１７．１７ａおよび
１７ｂの引取り導管、２０．２０ａおよび２０ｂの噴０
４器、および２３．２３ａおよび２３ｂの出口導管が設
けである。各引取り導管１７．１７ａおよび１７ｂには
冷却器２４、２４ａおよび２４ｂが備えられである。Each condensing section 13.13a and 13b has an extraction tray with reference number 15.
Four vessels, and outlet conduits 23.23a and 23b are provided. Each take-off conduit 17.17a and 17b is equipped with a cooler 24, 24a and 24b.
最上凝縮部１３はさらに付加噴ａＡ１２５を備えている
。連結管２７は付加噴ｒＪ４器２５を最上凝縮部の下に
配置の第１の凝縮部１３ａに付属の出口導管２３ａに連
結し、また連結管２８は付加噴射器２５を最上凝縮部の
下に配置の第２の凝縮部１３ｂに付属の出口導管２３ｂ
に連結する。The uppermost condensing section 13 further includes an additional jet aA125. A connecting pipe 27 connects the additional injector 25 to an outlet conduit 23a attached to the first condensing section 13a located below the uppermost condensing section, and a connecting pipe 28 connects the additional injector 25 below the uppermost condensing section. An outlet conduit 23b attached to the second condensing section 13b of the arrangement
Connect to.
塔頂出口導管９は、スチーム供給１！３２と出口管３６
を備えたスチームエジェクタ３０である真空ポンプと接
続される。The tower top outlet conduit 9 connects the steam supply 1!32 and the outlet pipe 36.
It is connected to a vacuum pump, which is a steam ejector 30 equipped with a steam ejector 30.
通常の操作では、炭化水素液体と炭化水素蒸気を含有す
る供給原料は供給原料供給導管４を通って蒸留塔１の入
口部３に３８０から４２５℃の温度で導入される。入口
部３に入ると、液体は流れから落下し、蒸留塔１の塔底
部６に集められ、ここから出口導管７を通り取り出され
る。In normal operation, a feed containing hydrocarbon liquid and hydrocarbon vapor is introduced through feed supply conduit 4 into inlet section 3 of distillation column 1 at a temperature of 380 to 425°C. Upon entering the inlet section 3, the liquid falls out of the stream and is collected in the bottom 6 of the distillation column 1, from where it is removed through the outlet conduit 7.
蒸気は３つの凝縮部１３ｂ、 １３ａおよび１３を通過
せしめられる。The steam is passed through three condensing sections 13b, 13a and 13.
凝縮部１３ｂでは２００から２８０℃の温度を有する冷
却液体が凝縮部１３ｂを通過する蒸気内に噴射される。In the condensing section 13b, a cooling liquid having a temperature of 200 to 280° C. is injected into the vapor passing through the condensing section 13b.
その結果、蒸気の１部は凝縮し抽出トレイ１５ｂに集め
られる。液体は引取り導管１７ｂを通り蒸留塔１から取
り出されるが、冷却器２４ｂで冷却される。取り出され
た液体の第１部分は噴射器２０ｂに送られ、取り出され
た液体の第２１１ｉＳ分は導管２８を通って噴射器２５
に送られ、残りは導管３５ｂを通り製品として取り出さ
れる。As a result, a portion of the steam condenses and is collected in extraction tray 15b. The liquid is withdrawn from the distillation column 1 through the take-off conduit 17b and is cooled in the cooler 24b. A first portion of the withdrawn liquid is sent to injector 20b and a 211iS portion of the withdrawn liquid is passed through conduit 28 to injector 25.
The remainder passes through conduit 35b and is taken out as a product.
凝縮部１３ａでは、１５０から２３０℃の温度を有する
冷却液体が蒸気内に噴射され、凝縮蒸気は抽出トレイ１
５ａに１められ、そこから引取り導管１７ａを通って取
り出され、且つ冷ＦＡ５２４ａで冷Ｎ１される。取り出
された液体の第１部分は噴１ｆｆｉ２０ａに送られ、取
り出された液体の第２部分は導管２７を通って噴射器２
５に送られ、残りは導管３５ａを通り製品として取り出
される。In the condensing section 13a, a cooling liquid having a temperature of 150 to 230° C. is injected into the steam, and the condensed steam flows into the extraction tray 1.
5a, from which it is taken out through take-off conduit 17a, and cooled in cold N1 by cold FA 524a. A first portion of the withdrawn liquid is sent to the injector 1ffi 20a and a second portion of the withdrawn liquid is passed through the conduit 27 to the injector 2.
5, and the remainder is taken out as a product through a conduit 35a.
凝縮部１３では、６０から １５０℃の温度を有する冷
部液体が同様に蒸気内に噴射され、凝縮蒸気は抽出トレ
イ１５に集められ、そこから引取り導管１７を通って取
り出され、且つ冷却器２４で冷却される。In the condensing section 13, a cold liquid with a temperature of 60 to 150° C. is likewise injected into the steam, the condensed steam being collected in an extraction tray 15, from where it is taken off through a take-off conduit 17 and in a cooler. It is cooled at 24.
取り出された液体の１部は噴射器２０に送られ、残りは
導管２３を通り製品として取り出される。A portion of the withdrawn liquid is sent to the injector 20 and the remainder is withdrawn as product through conduit 23.
最上凝縮部１３を通過する蒸気には、噴射器２０を通り
噴射される冷却液体に加うるに、６０から１５０℃の温
度を有する付加冷部液体がその蒸気内に噴射器２５を通
り噴射される。付加液体は、それに吸収された蒸気とと
もに導管１７を通り塔１から取り出されるが、またその
１部は導管２３を通り製品として取り出される。In addition to the cooling liquid injected through the injector 20, an additional cooling liquid having a temperature of 60 to 150° C. is injected into the vapor passing through the uppermost condensing section 13 through the injector 25. Ru. The additional liquid, together with the vapor absorbed therein, is removed from the column 1 through line 17, and a portion thereof is removed as product through line 23.
凝縮部１３．１３ａおよび１３ｂから凝縮した形で取り
出されなかった蒸気部は、塔１の塔頂部８からスチーム
エジェクタ３０の作用により塔頂出口導管９を通り取り
出される。そうする際に、スチームエジェクタは蒸留塔
１内を大気圧以下に保持する。The vapor fraction not removed in condensed form from the condensing sections 13.13a and 13b is removed from the top 8 of the column 1 through the top outlet conduit 9 by the action of a steam ejector 30. In doing so, the steam ejector maintains the interior of the distillation column 1 below atmospheric pressure.
噴ＯＡ器２５を通り噴射される付加冷却液体は炭化水素
蒸気を吸収することが見出されたが、さもない場合には
、これは出口導管９を通り塔１から取り出されるもので
あった。It was found that the additional cooling liquid injected through the injector OA device 25 absorbs hydrocarbon vapors that would otherwise be removed from the column 1 through the outlet conduit 9.
付加液体の聞は、真空ポンプにより取り出される蒸気部
分内の有用炭化水素の量が最小になるように選択される
。適切には、最上凝縮部内に噴射される冷部液体は、最
上凝縮部から取り出される液体幻当り、最上凝縮部より
下に配置の凝縮部より取り出される液体の０．５から
１ｋｇからなる。The length of the additional liquid is selected to minimize the amount of useful hydrocarbons in the vapor portion removed by the vacuum pump. Suitably, the cold liquid injected into the top condenser is equal to or less than 0.5 of the liquid drawn from a condenser located below the top condenser per drop of liquid drawn from the top condenser.
It consists of 1 kg.
図面を参照し説明した方法では、付加冷ＩＪ３液体は別
の噴射器２５を通り送られた。またはこの液体は導管１
１を通り送られる液体に付加し噴ａ４器２０を通り供給
することもできる。後者の場合には別の噴射器は不要で
ある。In the method described with reference to the figures, additional cold IJ3 liquid was sent through another injector 25. or this liquid is in conduit 1
It is also possible to add it to the liquid being sent through A4 1 and feed it through A4 jet 20. In the latter case a separate injector is not required.
添付図面は減圧蒸留塔１の縦断面概略図を示す。
１・・・・・・減圧蒸留塔、 ３・・・・・・入口部
、４・・・・・・供給原料供給導管、 ６・・・・・
・塔底部、７・・・・・・出口導管、 ８・・・・・
・塔頂部、９・・・・・・塔頂出口導管、 １３・・・
・・・（最上）凝縮部、１３ａ・・・・・・（第１）凝
縮部、
１３ｂ・・・・・・（第２）凝縮部、
１５、１５ａおよび１５ｂ・・・・・・抽出トレイ、１
７、１７ａおよび１７ｂ・・・・・・引取り導管、２０
、２０ａおよび２０ｂ・・・・・・噴射器、２３、２３
ａおよび２３ｂ・・・・・・出口導管、２４、２４ａお
よび２４ｂ・・・・・・冷却器、２５・・・・・・（付
加）噴射器、 ２７および２８・・・・・・連結管、３
０・・・・・・スチームエジェクタ、 ３２・・・・・
・スチーム供給管、 ３５ａおよび３５ｂ・・・・・・
導管、 ３６・・・・・・出口管。The accompanying drawing shows a schematic vertical cross-sectional view of a vacuum distillation column 1. DESCRIPTION OF SYMBOLS 1... Vacuum distillation column, 3... Inlet section, 4... Feed material supply conduit, 6...
・Tower bottom, 7... Outlet pipe, 8...
・Tower top, 9...Tower top outlet conduit, 13...
...(Top) condensing section, 13a...(first) condensing section, 13b...(second) condensing section, 15, 15a and 15b...extraction tray ,1
7, 17a and 17b...take-off conduit, 20
, 20a and 20b... Injector, 23, 23
a and 23b...outlet conduit, 24, 24a and 24b...cooler, 25...(additional) injector, 27 and 28...connecting pipe ,3
0...Steam ejector, 32...
・Steam supply pipe, 35a and 35b...
Conduit, 36... Outlet pipe.
Claims (4)
び蒸気を含有する供給原料を導入し、蒸留塔の塔底部か
ら液体を取り出し、蒸気を蒸留塔の入口部と塔頂部との
間に互いに上下に配置された少なくとも２つの凝縮部を
通過せしめ、塔頂部から蒸気を取り出し、各凝縮部内に
冷却液体を噴射し、且つ各凝縮部から液体を取り出すこ
とからなる減圧蒸留方法であつて、ここで各凝縮部内に
噴射する冷却液体はその凝縮部から取り出した液体から
なり、最上凝縮部内に噴射する冷却液体は最上凝縮部よ
り下に配置された凝縮部から取り出した液体をさらに含
むことを特徴とする減圧蒸留方法。(1) Introducing a feedstock containing liquid and vapor to the inlet of a distillation column operating below atmospheric pressure, removing the liquid from the bottom of the column, and discharging the vapor between the inlet and the top of the column. A vacuum distillation method comprising: passing through at least two condensing sections arranged one above the other, extracting vapor from the top of the column, injecting a cooling liquid into each condensing section, and removing liquid from each condensing section. , wherein the cooling liquid injected into each condensing section consists of the liquid taken out from the condensing section, and the cooling liquid injected into the uppermost condensing section further includes the liquid taken out from the condensing section arranged below the uppermost condensing section. A vacuum distillation method characterized by:
射する冷却液体は、最上凝縮部の下に配置された第１お
よび／または第２の凝縮部から取り出した液体をさらに
含有することを特徴とする請求項１に記載の減圧蒸留方
法。(2) The vapor passes through three condensing sections, and the cooling liquid injected into the top condensing section further contains liquid taken from the first and/or second condensing section arranged below the top condensing section. The reduced pressure distillation method according to claim 1, characterized in that:
から取り出される液体ｋｇ当り最上凝縮部の下に配置さ
れた凝縮部から取り出される液体の０．５から１ｋｇを
含むことを特徴とする請求項１または２に記載の減圧蒸
留方法。(3) The cooling liquid injected into the uppermost condensing section is characterized in that the cooling liquid injected into the uppermost condensing section contains from 0.5 to 1 kg of liquid taken out from the condensing section arranged below the uppermost condensing section per kg of liquid taken out from the uppermost condensing section. The reduced pressure distillation method according to claim 1 or 2.
１に記載の減圧蒸留方法。(4) The vacuum distillation method according to claim 1, substantially as described in the specification with reference to the accompanying drawings.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8903011.8 | 1989-02-10 | ||
| GB898903011A GB8903011D0 (en) | 1989-02-10 | 1989-02-10 | Vacuum distillation process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02241505A true JPH02241505A (en) | 1990-09-26 |
| JP3026574B2 JP3026574B2 (en) | 2000-03-27 |
Family
ID=10651463
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP02029354A Expired - Fee Related JP3026574B2 (en) | 1989-02-10 | 1990-02-08 | Vacuum distillation method |
Country Status (12)
| Country | Link |
|---|---|
| US (1) | US5019218A (en) |
| EP (1) | EP0382314B1 (en) |
| JP (1) | JP3026574B2 (en) |
| KR (1) | KR0144568B1 (en) |
| AU (1) | AU620494B2 (en) |
| CA (1) | CA2009571C (en) |
| DE (1) | DE69002957T2 (en) |
| ES (1) | ES2043239T3 (en) |
| GB (1) | GB8903011D0 (en) |
| MY (1) | MY106047A (en) |
| SA (1) | SA90100276B1 (en) |
| ZA (1) | ZA90930B (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES2043551B1 (en) * | 1992-05-18 | 1994-07-01 | Consejo Superior Investigacion | DEVICE FOR THE SEPARATION AND CONCENTRATION OF VOLATILE COMPONENTS OF THERMOSENSITIVE SAMPLES BY DISTILLATION AND SIMULTANEOUS EXTRACTION THROUGH ORGANIC SOLVENTS. |
| KR20010085113A (en) * | 2001-08-11 | 2001-09-07 | 임하빈 | The manufacturing apparatus for distilled water |
| NZ520365A (en) * | 2002-07-24 | 2004-12-24 | Distech Ltd | Vacuum sealing arrangement for a liquid concentrator |
| SE526792C2 (en) * | 2004-03-03 | 2005-11-08 | Tetra Laval Holdings & Finance | Apparatus for evaporative cooling of a liquid product |
| US7588664B2 (en) * | 2005-07-27 | 2009-09-15 | Chicago Bridge & Iron Company | Oil distillation vacuum column with thickened plate in the vapor horn section |
| CN104610999B (en) * | 2013-11-04 | 2017-05-24 | 中石化洛阳工程有限公司 | Underpressure distillation tower and underpressure distillation method |
| CN105233518A (en) * | 2015-10-16 | 2016-01-13 | 海南汉地阳光石油化工有限公司 | Fractionating tower, fractionating system and method for producing heat conducting oil |
| KR101854623B1 (en) | 2016-06-15 | 2018-05-04 | 베니트엠 주식회사 | Method for regenerating ammonium bicarbonate solution |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1854002A (en) * | 1927-09-06 | 1932-04-12 | Union Oil Co | Process and apparatus for rectifying vapors |
| US2224986A (en) * | 1938-03-05 | 1940-12-17 | Armour & Co | Fatty acid treatment |
| US2646392A (en) * | 1949-04-29 | 1953-07-21 | Universal Oil Prod Co | Apparatus for fractionating multicomponent streams |
| US2805981A (en) * | 1953-03-20 | 1957-09-10 | Phillips Petroleum Co | Process and apparatus for flash distillation |
| US2901425A (en) * | 1953-12-28 | 1959-08-25 | Phillips Petroleum Co | Vacuum distillation |
| US2885354A (en) * | 1954-12-30 | 1959-05-05 | Sun Oil Co | Distillation of petroleum hydrocarbons |
| DE1173431B (en) * | 1961-09-14 | 1964-07-09 | Basf Ag | Method and device for rectification or distillation of liquid mixtures |
| DE1519663A1 (en) * | 1966-03-16 | 1970-04-09 | Metallgesellschaft Ag | Multi-stage distillation and rectification process |
| DE3100005A1 (en) * | 1981-01-02 | 1982-08-05 | Achenbach Buschhütten GmbH, 5910 Kreuztal | RECTIFICATION COLON |
| CA1197806A (en) * | 1982-05-28 | 1985-12-10 | Pieter Van Der Heyden | Process for separating a multi-component liquid |
| SU1333688A1 (en) * | 1985-11-04 | 1987-08-30 | Производственное Объединение "Новополоцкнефтеоргсинтез" Им.Хху Съезда Кпсс | Method of producing fuel fractions |
| US4834868A (en) * | 1988-01-29 | 1989-05-30 | Breslube Usa, Inc. | Neutralizing oxidation product components in continuous rerefining of used oil stocks |
| US4894145A (en) * | 1988-07-19 | 1990-01-16 | Applied Automation, Inc. | Automatic control of feedstock vacuum towers |
-
1989
- 1989-02-10 GB GB898903011A patent/GB8903011D0/en active Pending
-
1990
- 1990-02-07 KR KR1019900001481A patent/KR0144568B1/en not_active IP Right Cessation
- 1990-02-07 DE DE90200278T patent/DE69002957T2/en not_active Expired - Fee Related
- 1990-02-07 US US07/476,183 patent/US5019218A/en not_active Expired - Fee Related
- 1990-02-07 EP EP90200278A patent/EP0382314B1/en not_active Expired - Lifetime
- 1990-02-07 ES ES90200278T patent/ES2043239T3/en not_active Expired - Lifetime
- 1990-02-08 CA CA002009571A patent/CA2009571C/en not_active Expired - Lifetime
- 1990-02-08 MY MYPI90000199A patent/MY106047A/en unknown
- 1990-02-08 AU AU49371/90A patent/AU620494B2/en not_active Ceased
- 1990-02-08 ZA ZA90930A patent/ZA90930B/en unknown
- 1990-02-08 JP JP02029354A patent/JP3026574B2/en not_active Expired - Fee Related
- 1990-06-11 SA SA90100276A patent/SA90100276B1/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| DE69002957D1 (en) | 1993-10-07 |
| KR900012650A (en) | 1990-09-01 |
| JP3026574B2 (en) | 2000-03-27 |
| ES2043239T3 (en) | 1993-12-16 |
| CA2009571C (en) | 2000-06-13 |
| SA90100276B1 (en) | 2003-04-28 |
| US5019218A (en) | 1991-05-28 |
| EP0382314A3 (en) | 1992-04-15 |
| CA2009571A1 (en) | 1990-08-10 |
| GB8903011D0 (en) | 1989-03-30 |
| ZA90930B (en) | 1990-10-31 |
| MY106047A (en) | 1995-03-31 |
| AU4937190A (en) | 1990-08-16 |
| EP0382314B1 (en) | 1993-09-01 |
| AU620494B2 (en) | 1992-02-20 |
| EP0382314A2 (en) | 1990-08-16 |
| KR0144568B1 (en) | 1998-07-15 |
| DE69002957T2 (en) | 1993-12-16 |
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